WO2022166116A1 - Procédé de production de trona - Google Patents

Procédé de production de trona Download PDF

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Publication number
WO2022166116A1
WO2022166116A1 PCT/CN2021/106179 CN2021106179W WO2022166116A1 WO 2022166116 A1 WO2022166116 A1 WO 2022166116A1 CN 2021106179 W CN2021106179 W CN 2021106179W WO 2022166116 A1 WO2022166116 A1 WO 2022166116A1
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Prior art keywords
sodium carbonate
brine
crystallization
concentrated
separation
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PCT/CN2021/106179
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English (en)
Chinese (zh)
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王吉刚
卢立祥
冯青天
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中国天辰工程有限公司
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Publication of WO2022166116A1 publication Critical patent/WO2022166116A1/fr
Priority to US18/061,994 priority Critical patent/US20230103792A1/en

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/12—Preparation of carbonates from bicarbonates or bicarbonate-containing product
    • C01D7/126—Multi-step processes, e.g. from trona to soda ash
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/10—Preparation of bicarbonates from carbonates
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/12—Preparation of carbonates from bicarbonates or bicarbonate-containing product
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/22—Purification
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/22—Purification
    • C01D7/24—Crystallisation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/22—Purification
    • C01D7/26—Purification by precipitation or adsorption
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/35—Varying the content of water of crystallisation or the specific gravity
    • C01D7/37—Densifying sodium carbonate

Definitions

  • the invention relates to the field of trona production, in particular to a trona production process.
  • Trona production mainly utilizes trona ore (Na 2 CO 3 ⁇ NaHCO 3 ⁇ 2H 2 O) or soda stone ore (NaHCO 3 ) after dissolving, and is obtained through the production process of sodium carbonate monohydrate.
  • US6589497 B2 discloses a process for producing trona.
  • a sodium carbonate product is obtained by brine stripping, evaporation, neutralization, monohydrate alkali crystallization, centrifugation and drying, and the mother liquor obtained by centrifugation is recycled through a decahydrate alkali process. The resulting mother liquor is discharged without further recycling.
  • US5283054 discloses a trona production process. After the brine is evaporated and stripped to decompose most of the sodium bicarbonate, the remaining sodium bicarbonate is neutralized with caustic soda, and then decahydrate is crystallized. The obtained decahydrate crystals are dissolved and used for Soda monohydrate is produced to obtain heavy soda ash. This process requires a large capacity of decahydrate alkali, and a large amount of mother liquor produced by separation of decahydrate alkali is at least partially discharged to prevent impurities from accumulating in the system and not fully recycled.
  • US7507388 B2 and CN 1772615A disclose a kind of trona production process, through brine purification and preheating, evaporation & stripping, monohydrate alkali crystallization, centrifugation, drying process to produce heavy sodium carbonate product, monohydrate alkali centrifugal mother liquor part through ten
  • the water-alkali process is recycled, and the other part is causticized and filtered to obtain a caustic soda solution, which is used for the production of decahydrate.
  • the mother liquor produced by the separation of the decahydrate base is discharged and is not used further.
  • the concentration of caustic soda solution obtained by causticization and filtration is relatively low, generally about 10%.
  • US9593023 B2 discloses a production process of sodium carbonate/sodium bicarbonate, the process obtains concentrated brine through brine pretreatment, wet decomposition, evaporation, and neutralization, and makes it crystallized in a monohydrate alkali crystallizer/sodium bicarbonate crystallizer, Sodium carbonate/sodium bicarbonate crystals are obtained by separation, and the separated discharge liquid is causticized and concentrated to obtain a NaOH solution with a concentration of more than 25 wt%, which is reused in the crystallization process or the upstream process of crystallization.
  • the process of causticizing and concentrating to prepare NaOH solution with a concentration of more than 25wt% can be used to treat the discharge liquid produced by the crystallization process of anhydrous alkali/monohydrate alkali/decahydrate alkali/sesqui alkali/sodalite.
  • the treatment of the effluent from the water alkali crystallizer defines that the raw material of the decahydrate alkali crystallizer comes from the discharge liquid of the monohydrate alkali crystallizer.
  • US7255841 B2 working condition is a kind of sodium bicarbonate production process, utilizes the discharge liquid produced by the monohydrate alkali process to carry out decahydrate crystallization, utilizes the obtained decahydrate alkali to produce sodium bicarbonate, and the process decahydrate alkali and sodium bicarbonate process produce
  • the total amount of discharged liquid is less than that of monohydrate alkali discharge liquid, which can effectively reduce the amount of waste liquid discharged from the system.
  • US9051627 discloses a process for producing sodium bicarbonate, the process utilizes an ammonium carbonate solution containing at least 2wt% of sodium chloride or sodium sulfate impurities to produce sodium bicarbonate, and the solution is partially derived from anhydrous alkali/monohydrate/heptahydrate/ Decahydrate/sesqui-alkali/sodalite crystallizer can also come from the discharge waste liquid of monohydrate alkali crystallizer. This process limits the content of sodium chloride or sodium sulfate impurities in the feedstock.
  • the present invention aims to propose a kind of trona production technology, through melt mining, pretreatment, stripping concentration, sodium carbonate decahydrate crystallization and separation, sodium carbonate decahydrate dissolving, sodium carbonate monohydrate crystallization and separation, a Steps such as drying with sodium carbonate obtain heavy soda ash; Utilize sodium carbonate decahydrate solution (brine 5) or concentrated brine 3, crystallize and separate through sodium bicarbonate, and dry sodium bicarbonate to obtain sodium bicarbonate product; The effluent 1 produced in the crystallization and separation process is causticized, evaporated and reused for the production of sodium carbonate; the causticized mud produced in the causticizing section is recycled to the causticizing section through calcination. Through this process, the maximum utilization of resources can be achieved.
  • a trona production process comprising the steps:
  • Dissolved mining inject well water into the mine (trona ore (Na 2 CO 3 ⁇ NaHCO 3 ⁇ 2H 2 O) or soda ore (NaHCO 3 ) or soda ash ore) to dissolve the sodium carbonate therein and/or sodium bicarbonate to obtain brine 1 containing sodium carbonate and/or sodium bicarbonate and other soluble salts; (or brine 1 comes from a salt lake or other underground brine, etc., and the brine contains sodium sulfate and/or sodium chloride such as soluble impurities, insoluble suspended solids and TOC)
  • Pretreatment removing the solid particles and/or TOC contained in the brine 1 to obtain the brine 2;
  • dissolving sodium carbonate decahydrate the obtained sodium carbonate decahydrate crystal is mixed with the solution from other steps to dissolve the crystal, and the solution obtained is divided into two parts, one part is brine 4, and the other part is brine 5;
  • brine 4 is concentrated by evaporation, crystallized in a sodium carbonate monohydrate crystallizer, and separated by crystal slurry to obtain low mother liquor residual sodium carbonate monohydrate crystals and discharge liquid 2;
  • the sodium carbonate monohydrate crystals are dried to obtain high-quality heavy soda ash;
  • the discharge liquid 2 is mixed with the concentrated brine 3, and after neutralization, it enters the sodium carbonate decahydrate crystallizer for crystallization and separation of sodium carbonate decahydrate;
  • the dilute NaOH solution will be obtained by evaporation and concentration. Due to the increase in concentration, some sodium chloride and/or sodium sulfate impurities in the dilute NaOH are crystallized. After removing the impurities, a concentrated NaOH solution is obtained, and the concentrated NaOH solution can be used for neutralization. Residual sodium bicarbonate in brine 3 was concentrated.
  • the condensate obtained from the stripping concentration and/or the crystallization and separation of sodium carbonate monohydrate can be used in the dissolution and mining step.
  • it also includes removing TOC contained in the system in the effluent 1 and/or removing TOC contained in the system in the obtained dilute NaOH solution or concentrated NaOH solution.
  • the TOC is removed by an activated carbon adsorption method, an ozone oxidation method or a resin adsorption method.
  • activated carbon adsorption is used.
  • the total alkalinity in the concentrated brine 3 is 22wt%-28wt% in terms of sodium carbonate.
  • the required solution of the sodium carbonate decahydrate dissolving step can be one or both of brine 2, the condensed liquid produced by the crystallization of steamed sodium carbonate and the separation step, and the primary stripping liquid of the stripping concentration step. above.
  • the CO produced in the stripping concentration step can be used for the carbonization reaction in the crystallization of sodium bicarbonate and the separation step;
  • the raw material required for the crystallization of sodium bicarbonate can also come from concentrated brine 3, or from concentrated brine 3 and brine 5. mixture.
  • the concentration of the concentrated NaOH solution produced by the evaporation step is 20wt%-35wt%; preferably, the concentration of the concentrated NaOH is 25wt%-30wt%.
  • the equipment in the described sodium carbonate decahydrate crystallization and separation step comprises a two-stage flasher and a first-stage crystallizer, and the mixture of concentrated brine 3 and discharge liquid 2 is crystallized out of the decahydrate in the crystallizer after the two-stage flasher in sequence.
  • Sodium carbonate; and a stirring mechanism is provided at the bottom of the secondary flasher and the crystallizer.
  • the ice machine system is used to provide cooling capacity, and the ice machine system is used to apply heat to the sodium carbonate decahydrate solution; in the ice machine system, the compressor outlet condenser is a two-stage condensing in series.
  • the first-stage condenser uses sodium carbonate decahydrate solution containing sodium carbonate decahydrate crystals as a cold source.
  • the pretreatment uses a sand filter to remove insoluble matter contained in the brine 1 .
  • the stripping concentration may include multiple stages, preferably, two-stage stripping and two-stage concentration.
  • the liquid from the first stripping tower is the first-stage stripping liquid.
  • the crystallization temperature of the sodium carbonate decahydrate is 15-30°C; the crystallization temperature of the sodium carbonate monohydrate is 35-109°C.
  • the process used in the evaporation step is three-effect evaporation or MVR
  • the soluble salt impurities contained in the system are at least partially discharged from the evaporation step crystallization
  • the soluble salt impurities contained in the system are sodium chloride and/or Sodium sulfate.
  • a centrifuge is used for the separation of sodium carbonate decahydrate crystals.
  • a centrifuge is used for the separation of sodium carbonate monohydrate crystals.
  • the ash milk required for causticization is generated by the reaction of CaO and ash water in the ash machine, and the ash water comes from one of brine 1, brine 2, and condensate or a mixture of any combination of ratios.
  • the caustic mud needs to be washed before calcination to control the Na ion content in the calciner feed; further, the washing equipment adopts a vacuum belt filter; further, the Na ion content in the calciner feed is controlled to be less than or equal to 0.5 wt%.
  • a rotary kiln is used for calcining the caustic mud.
  • the trona production process of the present invention has the following advantages:
  • trona production technique of the present invention is organically combined with sodium carbonate decahydrate production technique, sodium carbonate monohydrate production technique and causticization process caustic soda technique, for processing impurities such as sodium chloride/sodium sulfate
  • the trona ore or soda ore with high content can effectively reduce the sodium chloride/sodium sulfate in the sodium carbonate product by first producing sodium carbonate decahydrate, and then using the sodium carbonate decahydrate product to produce sodium carbonate monohydrate. impurity content.
  • the causticization treatment of the effluent produced in the production process of sodium carbonate decahydrate is carried out to obtain caustic soda, which is reused in the production process of sodium carbonate decahydrate to realize the reduction of discharge, and at the same time, the resources in the effluent are recycled. It can also solve the problem of outsourcing caustic soda required in trona production in remote areas.
  • the trona production technique of the present invention in the sodium carbonate decahydrate crystallization and separation step, adopts the technique of two-stage series-connected flash evaporation and crystallization, the flash evaporation and crystallization operation pressure are reduced step by step, and the flash evaporation of each level is controlled.
  • the amount of steam is beneficial to crystallization, and the formation of crystals during the crystallization process can be better controlled by cascade flash evaporation.
  • the secondary flasher and the crystallizer creatively use the bottom stirring form, which makes the liquid level in the secondary flasher and the crystallizer refresh faster, accelerates the removal of water, and at the same time is beneficial to the enlargement of the crystal particle size.
  • (3) trona production technique of the present invention adopts the technique of two-stage series condensing in the ice machine system used in sodium carbonate decahydrate crystallization and separation step, wherein, the first-stage condenser utilizes the band sodium carbonate decahydrate crystal
  • the dissolved sodium carbonate decahydrate solution is used as a cold source, which not only reduces the amount of circulating water, but also provides heat for the dissolution of sodium carbonate decahydrate crystals by the condenser. Through thermal coupling, the energy consumption of the system is effectively reduced.
  • trona production technique of the present invention adopts sodium carbonate decahydrate dissolving solution for sodium bicarbonate production, compared with prior art adopting concentrated brine to carry out sodium bicarbonate production technique, sodium carbonate decahydrate dissolving liquid is especially
  • the content of impurities such as sodium chloride/sodium sulfate in the sodium carbonate decahydrate solution dissolved by the condensate is lower, so that the final product sodium bicarbonate has less impurities and better quality.
  • Fig. 1 is the flow chart of the trona production process described in the embodiment of the present invention.
  • Embodiment (1) is a diagrammatic representation of Embodiment (1).
  • a kind of trona production process comprises the steps:
  • TSS Total Suspended Solids
  • the brine 2 is subjected to two-stage stripping and concentration to obtain concentrated brine 3, which is mainly composed of Na 2 CO 3 : 21-24 wt %, NaHCO 3 : 1.5-3 wt %, NaCl: 2.02 wt %, Na 2 SO 4 : 0.15 wt%.
  • concentrated brine 3 enters sodium carbonate decahydrate crystallization and separation operation after the neutralization of concentrated NaOH solution, obtains 1078t/h sodium carbonate decahydrate crystal, produces 330t/h discharge liquid 1 simultaneously,
  • the main composition of the discharge liquid 1 is Na 2 CO 3 : 11-15 wt %, NaHCO 3 : 0-1 wt %, NaCl: 8.5-13 wt %, and Na 2 SO 4 : 0.8-1.4 wt %.
  • the equipment in the crystallization of sodium carbonate decahydrate and the separation step includes a two-stage flasher and a first-stage crystallizer, and the mixture of concentrated brine 3 and discharge liquid 2 is sequentially passed through the two-stage flasher in the crystallizer.
  • the sodium carbonate decahydrate is crystallized in the crystallizer.
  • the bottom of the secondary flasher and the crystallizer are provided with a stirring mechanism.
  • the process of two-stage flash evaporation and crystallization in series the pressure of flash evaporation and crystallization operation is reduced in steps, and the amount of flash evaporation in each stage is controlled, which is beneficial to crystallization.
  • the formation of crystals in the crystallization process can be better controlled .
  • the secondary flasher and the crystallizer creatively use the bottom stirring form, which makes the liquid level in the secondary flasher and the crystallizer refresh faster, accelerates the removal of water, and at the same time is beneficial to the enlargement of the crystal particle size.
  • the ice machine system In the crystallization and separation steps of sodium carbonate decahydrate, the ice machine system is used to provide cold energy, and the ice machine system is used to apply heat to the sodium carbonate decahydrate solution; the compressor outlet condenser in the ice machine system is a two-stage series-connected condenser, Among them, the first-stage condenser uses the sodium carbonate decahydrate solution containing sodium carbonate decahydrate crystals as a cold source.
  • a two-stage series condensation process is adopted, in which the first-stage condenser uses sodium carbonate decahydrate solution with sodium carbonate decahydrate crystals as a cold source, which not only reduces the amount of circulating water, but also provides heat for decahydrate.
  • the dissolution of sodium carbonate crystals effectively reduces the energy consumption of the system through thermal coupling.
  • dissolving sodium carbonate decahydrate adopt the first-stage stripping liquid from the stripping concentration step to dissolve sodium carbonate decahydrate, and obtain about 1660t/h total alkalinity (calculated in sodium carbonate) as 27 ⁇ 30wt% decahydrate Sodium carbonate solution, of which about 1570t/h is used as brine 4 for the production of sodium carbonate monohydrate, and the rest is used as brine 5 for the production of sodium bicarbonate.
  • the sodium carbonate monohydrate crystals are dried to obtain 316t/h sodium carbonate product, wherein the sodium carbonate content is 99.79%, and the sodium chloride content is less than 1000ppm.
  • the mixture of the obtained discharge liquid 2 and concentrated brine 3 enters the crystallization and separation process of sodium carbonate decahydrate after neutralization.
  • the sodium carbonate decahydrate solution is used for the production of sodium bicarbonate. Compared with the prior art using concentrated brine for the production of sodium bicarbonate, the sodium carbonate decahydrate solution has a lower content of impurities such as sodium chloride/sodium sulfate, so that the The final product sodium bicarbonate has less impurities and better quality.
  • the caustic mud needs to be washed before calcination to control the Na ion content in the calciner feed; the washing equipment adopts a vacuum belt filter, and the Na ion content in the calciner feed is controlled to be less than or equal to 0.5wt%.
  • Rotary kiln is used for calcining of caustic mud.
  • the total sodium from trona ore is about 174t/h
  • the output sodium carbonate is 316.8t/h
  • sodium bicarbonate is 25.3t/h
  • about 45t/h sodium carbonate is returned to trona ore with injection well water for dissolution mining. , the rest of the sodium is lost in the production process.
  • the utilization efficiency of sodium is about 94.2%.
  • Embodiment (2) is a diagrammatic representation of Embodiment (2)
  • a kind of trona production process comprises the steps:
  • TSS Total Suspended Solids
  • the brine 2 is subjected to two-stage stripping and concentration to obtain concentrated brine 3, which is mainly composed of Na 2 CO 3 : 21-24 wt %, NaHCO 3 : 1.5-3 wt %, NaCl: 1.7 wt %, Na 2 SO 4 : 0.16 wt%.
  • concentrated brine 3 enters sodium carbonate decahydrate crystallization and separation operation after the neutralization of concentrated NaOH solution, obtains 1000t/h sodium carbonate decahydrate crystal, produces 258t/h discharge liquid 1 simultaneously,
  • the main composition of the discharge liquid 1 is Na 2 CO 3 : 11-15 wt %, NaHCO 3 : 0-1 wt %, NaCl: 8.5-13 wt %, and Na 2 SO 4 : 0.8-1.4 wt %.
  • dissolving of sodium carbonate decahydrate adopt the first-stage stripping liquid from the stripping and concentration step to dissolve sodium carbonate decahydrate, and obtain about 1500t/h total alkalinity (calculated as sodium carbonate) and be 27 ⁇ 30wt% decahydrate Sodium carbonate solution, of which about 1410t/h is used as brine 4 for the production of sodium carbonate monohydrate, and the rest is used as brine 5 for the production of sodium bicarbonate.
  • the sodium carbonate monohydrate crystals are dried to obtain 316t/h sodium carbonate product, wherein the sodium carbonate content is 99.79%, and the sodium chloride content is less than 1000ppm.
  • the mixture of the obtained discharge liquid 2 and concentrated brine 3 enters the crystallization and separation process of sodium carbonate decahydrate after neutralization.
  • the caustic mud needs to be washed before calcination to control the Na ion content in the calciner feed; the washing equipment adopts a vacuum belt filter, and the Na ion content in the calciner feed is controlled to be less than or equal to 0.5wt%.
  • Rotary kiln is used for calcining of caustic mud.
  • the production process is about 170t/h of total sodium from trona ore, producing 316.8t/h of sodium carbonate, 25.3t/h of sodium bicarbonate, and about 45t/h of sodium carbonate returned to trona ore with injection well water for dissolution mining , the rest of the sodium is lost in the production process.
  • the utilization efficiency of sodium is about 96.5%.
  • step (1) produce the same sodium carbonate and sodium bicarbonate product, can produce about 330t/h waste liquid, wherein containing about 43t/h of sodium carbonate, sodium bicarbonate 2.3 t/h.
  • step (1) produce the same sodium carbonate and sodium bicarbonate product, can produce about 330t/h waste liquid, wherein containing about 43t/h of sodium carbonate, sodium bicarbonate 2.3 t/h.
  • about 23t/h of caustic soda (100% NaOH content) needs to be consumed in the production process, and about 31t/h of sodium carbonate is additionally consumed for the preparation of caustic soda.
  • the utilization efficiency of sodium is about 87.8%.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Treating Waste Gases (AREA)

Abstract

La présente invention concerne un procédé de production de trona. Les étapes d'extraction par dissolution, de prétraitement, de stripping à la vapeur et de concentration, de cristallisation et de séparation de décahydrate de carbonate de sodium, de dissolution de décahydrate de carbonate de sodium, de cristallisation et de séparation de monohydrate de carbonate de sodium, et de séchage de monohydrate de carbonate de sodium sont effectuées pour obtenir du carbonate de sodium dense ; au moyen de la solution de décahydrate de carbonate de sodium ou de saumure concentrée 3, la cristallisation et la séparation de bicarbonate de sodium et le séchage de bicarbonate de sodium sont effectués pour obtenir un produit de bicarbonate de sodium ; un liquide de décharge 1 produit dans la procédure de cristallisation et de séparation de décahydrate de carbonate de sodium est recyclé pour la production de carbonate de sodium par caustification et évaporation ; la suspension caustifiée produite dans la section de caustification est recyclée dans une section de caustification par calcination. L'utilisation maximale des ressources peut être obtenue au moyen du procédé.
PCT/CN2021/106179 2021-02-03 2021-07-14 Procédé de production de trona WO2022166116A1 (fr)

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CN112850753B (zh) * 2021-02-03 2022-06-14 中国天辰工程有限公司 一种天然碱生产工艺
CN113321259A (zh) * 2021-04-16 2021-08-31 天华化工机械及自动化研究设计院有限公司 一种pta氧化尾气洗涤塔排出液的节能脱碳方法和系统
CN114560479A (zh) * 2022-04-19 2022-05-31 山东凯泰科技股份有限公司 一种纯碱生产系统及其生产工艺
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CN1772615A (zh) * 2004-11-11 2006-05-17 Eti化学和电气产品制造有限公司 由含碳酸氢盐的溶液制备重苏打、轻苏打、碳酸氢钠和硅酸钠的方法
CN104628014A (zh) * 2013-11-12 2015-05-20 索尔维公司 用于处理一种碳酸钠清洗液的方法
CN112850753A (zh) * 2021-02-03 2021-05-28 中国天辰工程有限公司 一种天然碱生产工艺

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